CN1139934A - Process for the (co) polymerization of olefins - Google Patents

Process for the (co) polymerization of olefins Download PDF

Info

Publication number
CN1139934A
CN1139934A CN95191444A CN95191444A CN1139934A CN 1139934 A CN1139934 A CN 1139934A CN 95191444 A CN95191444 A CN 95191444A CN 95191444 A CN95191444 A CN 95191444A CN 1139934 A CN1139934 A CN 1139934A
Authority
CN
China
Prior art keywords
mcl
ind
compound
carbon atom
accordance
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN95191444A
Other languages
Chinese (zh)
Other versions
CN1070505C (en
Inventor
G·科林纳
T·达洛科
M·加林贝蒂
E·阿尔比扎蒂
L·诺力斯蒂
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Spherilene SRL
Original Assignee
Spherilene SRL
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Spherilene SRL filed Critical Spherilene SRL
Publication of CN1139934A publication Critical patent/CN1139934A/en
Application granted granted Critical
Publication of CN1070505C publication Critical patent/CN1070505C/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F297/00—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer
    • C08F297/06—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the coordination type
    • C08F297/08—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the coordination type polymerising mono-olefins
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/04—Monomers containing three or four carbon atoms
    • C08F10/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/642—Component covered by group C08F4/64 with an organo-aluminium compound
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/04—Monomers containing three or four carbon atoms
    • C08F110/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2410/00—Features related to the catalyst preparation, the catalyst use or to the deactivation of the catalyst
    • C08F2410/05—Transitioning, i.e. transition from one catalyst to another with use of a deactivating agent
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65912—Component covered by group C08F4/64 containing a transition metal-carbon bond in combination with an organoaluminium compound

Abstract

Multistage process for the polymerization of one or more olefins of the formula CH2=CHR, in which R is hydrogen or an alkyl, cycloalkyl or aryl group having from 1 to 10 carbon atoms, comprising: (A) a first stage of polymerization, in which a first olefin polymer is prepared in the presence of titanium catalyst or vanadium catalyst; (B) a treatment stage in which the catalyst used previously is deactivated and in which a metallocene compound is supported on the olefin polymer produced in stage (A); and (C) a second stage of polymerization in which one or more olefins are polymerized in the presence of the product obtained from stage (B).

Description

Alkene (being total to) polymerization process
The present invention relates to the alkene CH that in two or more reactors, carries out 2The method of the multistep polymerization of=CHR (wherein R is hydrogen or alkyl, cycloalkyl or the aryl that contains 1-10 carbon atom).In at least one reactor, one or more described alkene carry out polymerization in the presence of the catalyzer of alkylaluminium cpd and the reaction product that is stated from Ti on the magnesium halide in active and/or V compound and obtain olefin polymer containing.In at least one other reactor, in case the catalyst system inactivation in first reactor, one or more described alkene CH 2=CHR is just carrying out polymerization by described olefin polymer is contacted with the compound of the transition metal M that contains at least one M-π key in the presence of the product that obtains, directly obtain new polymer composition in reactor.
The alkene multistep polymerization technology of carrying out in two or several reactors is known in patent documentation, and have special significance in industrial practice.Because in arbitrary reactor, might change the concentration of processing parameter such as temperature, pressure, monomer type and concentration, hydrogen or other molecular weight regulator independently, so multistep polymerization is much more flexible than one-step polymerization method at the composition and the aspect of performance of control final product.
When carrying out multistep polymerization usually, be in different step/reactors, to use same catalyzer: directly deliver to next step/reactor after the product discharging that in a reactor, obtains, and do not change the character of catalyzer.
Multistep processes can be used for for example preparing alkene (being total to) polymkeric substance of wide molecular weight distribution (MWD), and method is the polymerization species that generate various different molecular weights in different reactors.Molecular weight in each reactor also be we can say the scope of the MWD of final product, usually can be with molecular weight regulator (the being preferably hydrogen) control of different concns.The sequential polymerization method of the mixture by propylene and propylene and ethene, multistep processes also can be used to prepare high-impact propylene copolymer.In the first step, propylene homopolymerization or obtain the polymkeric substance of stereoregular: in second step with small amount of ethylene and/or the olefin-copolymerization that contains 4-10 carbon atom, polymerization in the presence of the polymkeric substance that contains catalyzer that the mixture of ethene and propylene obtains when the first step obtains the improved polypropene composition of shock strength.
This class technology is for example having narration in the United States Patent (USP) 4,521,566.In described patent, polypropene composition with high impact prepares with multistep processes, this method comprises that to have a step at least be the homopolymerization of propylene and has one at least to go on foot be the polymerization of ethylene/propylene mixture, and this two-stage polymerization all is to carry out containing in the presence of the catalyzer that is stated from the titanium compound on the magnesium halide in active.
European patent application EP-A-433989 has described a kind of preparation and has contained the method that 20-99% (weight) wherein comprises the polypropene composition of crystallization (being total to) polymkeric substance of at least 95% (weight) propylene units and the amorphous ethylene/propene copolymer that 1-80% (weight) wherein comprises 20-90% (weight) ethylene unit.This method is carried out in two steps: the first step is carried out in propylene liquid, generates crystalline polypropylene (being total to) polymkeric substance; Second step carried out in hydrocarbon solvent, generated the amorphous ethylene/propene copolymer.In two steps, the catalyzer that used catalyzer is all luxuriant by chiral metal and aikyiaiurnirsoxan beta is formed.
European patent application EP-A-433990 described with two step method preparation and EP-A-433989 described similar be the polymer based composition with the propylene, wherein crystalline polypropylene (being total to) polymkeric substance polymerization and making in propylene liquid in the first step, and the amorphous ethylene/propene copolymer made by vapour phase polymerization in second step.Equally, all use same and catalyzer that aikyiaiurnirsoxan beta form luxuriant in two reactors by chiral metal.
German patent application DE4130429 has described a kind of multistep processes of the preparation segmented copolymer that carries out fully in gas phase.The parent that preparation is made up of alfon or multipolymer in the first step, its amount is the 45-95% of gross product (weight): described in front polypropylene parent of second step and the catalyzer that is included in wherein exist preparation down to contain the multipolymer of the ethylene/alpha-olefin of 0.1-79.9% (weight) ethylene unit, and its amount is the 5-55% of gross product (weight).In above-mentioned two steps all is to carry out polymerization with same metalloscene catalyst in gas phase.
These methods of prior art have many deficiencies, and one of them is in different processing steps to use identical catalyzer, thereby always best in the characteristic of each step products therefrom.For example, prepare in the multistep processes with titanium catalyst under the situation of non-homogeneous copolymer, the performance of the rubbery copolymer that second step made is just relatively poor.In fact, known that the ethylene/propene copolymer made from titanium catalyst contains the long unitary segment of same monomer, so the elasticity of product is just relatively poor.
Have now found that, in the different step of multistep processes, use different catalyst systems might make the olefin polymer compositions of wide region.Specifically, method of the present invention comprises: the first step prepares olefin polymer in the presence of titanium catalyst or vanadium catalyst; Second step was the catalyst deactivation that makes the first step used; The 3rd step be described olefin polymer and contain the compound of the transition metal M that is selected from Ti, Zr, V or Hf of at least one M-π key and/or its reaction product in the presence of, make one or more olefinic polymerizations, described alkene can be identical or different with polymeric alkene in the first step.
The inventive method is characterised in that it comprises:
(A) the first step polymerization, wherein one or more described alkene CH 2=CHR aggregates into olefin homo or multipolymer in one or several reactor in the presence of catalyzer, described catalyzer contains alkylaluminium cpd and the transition metal M that is selected from Ti and V that contains no M-π key ICompound and the reaction product between the solids component of magnesium halide in active;
(B) treatment step, wherein the product that first polymerization procedure (A) is obtained is with any order:
(a) contact with the compound that can make the middle catalyst deactivation that exists of described step (A);
(b) contact with optional alkylaluminium cpd with the compound of the filtering metal M that is selected from Ti, Zr, V or Hf that contains at least one M-π key;
(C) the second step polymerization, wherein one or more described alkene carry out polymerization in one or several reactor in the presence of the product that described treatment step obtains.
In a preferred specific embodiments, the homopolymer or the multipolymer that make in first polymerization procedure (A) have porousness, and % represents by porosity, greater than 5%, are preferably greater than 10%, more preferably greater than 15%.
Best, the polymkeric substance that first polymerization procedure (A) makes has the feature of macroporosity.Usually, in the described polymkeric substance aperture of the hole more than 40% greater than 10000 .
Measure by following mercury method with porousness and pore size distribution that porosity is represented.
When preparation in step (C) during rubbery copolymer,, make it in gas phase, to react and do not have a special problem in the porousness of the prepared polymkeric substance of first polymerization procedure (A).
The amount of the polymkeric substance that first polymerization procedure (A) obtains is preferably greater than 2000g/g, more preferably greater than 3000g/g usually greater than the 1000g/g solid ingredient.
The amount of the polymkeric substance that first polymerization procedure (A) obtains preferably account for step (A) and (C) in the 10-90% (weight) of the polymkeric substance total amount that obtains, more preferably 20-80% (weight).
Used catalyzer contains the reaction product between following two components in first polymerization procedure (A):
(i) a kind of contain be selected from Ti and V do not contain M IThe transition metal M of-π key ICompound be stated from solid ingredient on the magnesium halide in active.This solid ingredient also can contain to electron compound (interior electron donor(ED)).In general, when solid ingredient is as propylene, 1-butylene and similarly will use interior electron donor(ED) during the stereoregular polymeric catalyzer of alpha-olefin, the higher tacticity of needs this moment is higher than 90 polymkeric substance so that obtain isotactic index.
(ii) a kind of alkylaluminium cpd and optional a kind of electronic donor compound capable (external electronic donor).
When preparation stereoregular polymer in the first step polymerization (I), for example during the propene polymer of high isotactic index, external electronic donor is used for giving the tacticity of catalyzer necessity.But when with as described two ethers of European patent EP-A-361493 during as interior electron donor(ED), the tacticity of catalyst themselves is height enough, so needs external electronic donor.
Magnesium halide in active is preferably MgCl 2, as the carrier of Zieglev-Natta catalyzer, this is widely known by the people in patent documentation.United States Patent (USP) 4,298,718 and 4,495,338 at first report these compounds are used for the Zieglev-Natta catalyzer.By these patents as can be known, be used as the carrier of olefin polymerization catalyst components or help the magnesium halide in active of carrier to characterize by the X-beta ray spectrum, the intensity of the strongest diffracted ray that usually occurs in disactivation halogenide spectrogram in this X-ray spectrogram has weakened, and replaced by halogen, the maximum strength position of halogen is compared with the strongest position alignment diffraction, moves to lower diffraction angle direction.
Transition metal M ICompound preferably be selected from: the alcoholate of halogenated titanium, halogen-titanium, VCl 3VCl 4, VOCl 3, halogen-vanadium alcoholate.
In the compound of titanium, TiCl preferably 4, TiCl 3With formula Ti (OR I) mX nThe alcoholate of halogen-titanium, R in the formula IBe alkyl or the COR that contains 1-12 carbon atom IGroup, X are halogens, (m+n) are the valence mumbers of titanium.
Catalyst component (i) is the spheroidal particle of the about 10-150 μ of mean diameter m preferably.The appropriate methodology for preparing the described component of particulate spherical in shape can be referring to for example patent EP-A-395083, EP-A-553805, EP-A-553806, and the content that the relevant preparation method of these patents and product characterize all at this as a reference.
The example of interior electron donor(ED) comprises the described ethers of patent EP-A-361493, EP-A-361494, EP-A-362705 and EP-A-451645, ester class, particularly polycarboxylic ester class, amine, ketone and 1,3-two ethers.
Alkylaluminium cpd (ii) is selected from trialkyl aluminium compound usually, for example triethyl aluminum, triisobutyl aluminium, three n-butylaluminum, tri-n-hexyl aluminum, tri-n-octylaluminium.Also can use the mixture such as the AlEt of trialkylaluminium and aluminum alkyl halide, alkyl aluminum hydride or alkylaluminium sesquichloride 2Cl and Al 2Et 3Cl 3
External electronic donor can be identical or different with interior electron donor(ED).When interior electron donor(ED) was polycarboxylic ester such as phthalic ester, external electronic donor preferably was selected from formula R 1R 2Si (OR) 2Silicon compound, R in the formula 1And R 2Be alkyl, cycloalkyl or the aryl that contains 1-18 carbon atom.The example of this silane has methylcyclohexyl dimethoxy silane, dimethoxydiphenylsilane, methyl-t-butyldimethoxysilane, dicyclopentyl dimethoxyl silane.
The compound of used transition metal M is the compound that is selected from Ti, the V, Zr and the Hf that contain at least one M-π key in treatment step (b).Best, described compound contains at least one and has monocycle or the polynuclear plane that contains conjugated pi electron, and with metal M coordinate ligand L.
The compound of described Ti, V, Zr or Hf preferably is selected from the component with following array structure:
Cp IMR 1 aR 2 bR 3 c????????(I)
Cp ICp IIMR 1 aR 2 b???????(II)
(Cp I-A e-Cp II) MR 1 aR 2 b(III) wherein M is Ti, V, Zr and Hf; Cp IAnd Cp IICan be identical or different, can be the cyclopentadienyl group of cyclopentadienyl group or replacement; Two or more substituting groups on described cyclopentadienyl group can form the ring R of one or more 4-6 of containing carbon atom 1, R 2And R 3Can be identical or inequality, can be hydrogen atom, halogen, contain alkyl or alkoxyl group, aryl, the alkaryl that contains 6-20 carbon atom or the aralkyl of 1-20 carbon atom, contain acyloxy, the allyl group of 1-20 carbon atom, the substituting group of silicon atoms; A is alkenyl bridge or is selected from the group with following array structure: =BR 1, AlR 1,-Ge-,-Sn-,-O-,-S-,=SO ,=SO 2,=NR 1,=PR 1,=P (O) R 1, M wherein 1Be Si, Ge or Sn; R 1And R 2Can be identical or inequality, can be the alkyl that contains 1-4 carbon atom or contain the aryl of 6-10 carbon atom; A, b, c are the integer of 0-4 independently; E is the integer of 1-6, two or several R 1, R 2And R 3Group can form a ring.When the Cp group was substituted, substituting group preferably contained the alkyl of 1-20 carbon atom.
The representative compounds of formula (I) comprising: (Me 5Cp) MMe 3, (Me 5Cp) M (OMe) 3, (Me 5Cp) MCl 3, (Cp) MCl 3, (Cp) MMe 3, (MeCp) MMe 3, (Me 3Cp) MMe 3, (Me 4Cp) MCl 3, (Ind) MBenz 3, (H 4Ind) MBenz 3, (Cp) MBu 3
The representative compounds of formula (II) comprising: (Cp) 2MMe 2, (Cp) 2MPh 2, (Cp) 2MEt 2, (Cp) 2MCl 2, (Cp) 2M (OMe) 2, (Cp) 2M (OMe) Cl, (MeCp) 2MCl 2, (Me 5Cp) 2MCl 2, (Me 5Cp) 2MMe 2, (Me 5Cp) 2MMeCl, (Cp) (Me 5Cp) MCl 2, (1-MeFlu) 2MCl 2, (BuCp) 2MCl 2, (Me 3Cp) 2MCl 2, (Me 4Cp) 2MCl 2, (Me 5Cp) 2M (OMe) 2, (Me 5Cp) 2M (OH) Cl, (Me 5Cp) 2M (OH) 2, (Me 5Cp) 2M (C 5H 5) 2, (Me 5Cp) 2M (CH 3) Cl, (EtMe 4Cp) 2MCl 2, [(C 6H 5) Me 4Cp] 2MCl 2, (Et 5Cp) 2MCl 2, (Me 5Cp) 2M (C 6H 5) Cl, (Ind) 2MCl 2, (Ind) 2MMe 2, (H 4Ind) 2MCl 2, (H 4Ind) 2MMe 2, { [Si (CH 3) 3] Cp} 2MCl 2, { [Si (CH 3) 3] 2Cp} 2MCl 2, (Me 4Cp) (Me 5Cp) MCl 2
The representative compound of Shi (III) comprises: C2H 4(Ind) 2MCl 2，C 2H 4(Ind) 2MMe 2，C 2H 4(H 4Ind) 2MCl 2，C 2H 4(H 4Ind) 2MMe 2， Me 2Si(Me 4Cp) 2MCl 2，Me 2Si(Me 4Cp) 2MMe 2，Me 2SiCp 2MCl 2，Me 2SiCp 2MMe 2， Me 2Si(Me 4Cp) 2MMeOMe，Me 2Si(Flu) 2MCl 2，Me 2Si(2-Et-5-iPrCp) 2MCl 2， Me 2Si(H 4Ind) 2MCl 2，Me 2Si(H 4Flu) 2MCl 2，Me 2SiCH 2(Ind) 2MCl 2， Me 2Si(2-Me-H 4Ind) 2MCl 2，Me 2Si(2-MeInd) 2MCl 2，Me 2Si(2-Et-5-ipr-Cp) 2MCl 2， Me 2Si(2-Me-5-EtCp) 2MCl 2，Me 2Si(2-Me-5-Me-Cp) 2MCl 2，Me 2Si (2-Me-4,5-benzindene base)2MCl 2，Me 2Si (4,5-benzindene base)2MCl 2，Me 2Si(2-EtInd) 2MCl 2， Me 2Si(2-ipr-Ind) 2MCl 2，Me 2Si (the MCl of 2-Shu butyl-Ind)2， Me 2Si (3-Shu butyl-5-MeCp)2MCl 2，Me 2Si (3-Shu butyl-5-MeCp)2MMe 2， Me 2Si(2-MeInd) 2MCl 2，C 2H 4(2-Me-4,5-benzindene base)2MCl 2， Me 2C(Flu)CpMCl 2，Ph 2Si(Ind) 2MCl 2，Ph(Me)Si(Ind) 2MCl 2， C 2H 4(H 4Ind)M(NMe 2) OMe, isopropylidene-((Flu) MCl of 3-Shu butyl-Cp)2， Me 2C(Me 4Cp)(MeCp)MCl 2，MeSi(Ind) 2MCl 2，Me 2Si(Ind) 2MMe 2， Me 2Si(Me 4Cp) 2MCI(OEt)，C 2H 4(Ind) 2M(NMe 2) 2，C 2H 4(Me 4Cp) 2MCl 2， C 2Me 4(Ind) 2MCl 2，Me 2Si(3-Me-Ind) 2MCl 2，C 2H 4(2-Me-Ind) 2MCl 2， C 2H 4(3-Me-Ind) 2MCl 2，C 2H 4(4，7-Me 2-Ind) 2MCl 2，C 2H 4(5，6-Me 2-Ind) 2MCl 2， C 2H 4(2，4，7-Me 3Ind) 2MCl 2，C 2H 4(3，4，7-Me 3Ind) 2MCl 2， C 2H 4(2-Me-H 4Ind) 2MCl 2，C 2H 4(4，7-Me 2-H 4Ind) 2MCl 2， C 2H 4(2，4，7-Me 3-H 4Ind) 2MCl 2，Me 2Si(4，7-Me 2-Ind) 2MCl 2，Me 2Si(5，6-Me 2-Ind) 2MCl 2， Me 2Si(2，4，7-Me 3-H 4Ind) 2MCl 2。
The meaning of symbol is as follows in the above-mentioned simplified style: Me=methyl, Et=ethyl, iPr=sec.-propyl, Bu=butyl, Ph=phenyl, Cp=cyclopentadienyl, Ind=indenyl, H 4Ind=4,5,6,7-tetrahydro indenyl, Flu=fluorenyl, Benz phenmethyl, M=Ti, Zr or Hf are preferably Zr.
Me 2Si (2-Me-Ind) 2ZrCl 2And Me 2Si (2-Me-H 4Ind) ZrCl 2Type compound and method for making thereof can be respectively referring to European patent application EP-A-485822 and 485820, and the content of these patents at this as a reference.
Me 2Si (the 3-tertiary butyl-5-MeCp) 2ZrCl 2And Me 2Si (2-Me-4,5-benzo indenyl) ZrCl 2Type compound and method for making thereof can be respectively referring to United States Patent (USP)s 5,132, and 262 and European patent application EP-A-549900, the content of these patents is at this as a reference.
First polymerization procedure (A) can carry out in liquid phase or gas phase in one or more reactors.Liquid phase can be made of (suspension method) inert hydrocarbon solvent, also can be by one or more alkene CH 2=CHR forms (liquid monomer method).Vapour phase polymerization can be carried out in fluidized-bed of knowing or mechanical stirring bed.
Treatment step (B) preferably carries out in two steps, (a) compound of the catalyst deactivation of using at first making polymkeric substance that polymerization procedure (A) makes and making described step (A) contacts, and (b) product that (a) obtained contacts with the solution of transition metal M in varsol (benzene, toluene, heptane, hexane, propylene liquid etc.) then.
The used optional self-drifting of examples for compounds of treatment step (a) is R Y-1The compound of XH, R is hydrogen or the alkyl that contains 1-10 carbon atom in the formula, and X is O, N or S, and y is the valence mumber of X.
The limiting examples of this compound comprises alcohols, thio-alcohol, list or dialkyl amine, NH 3, H 2O and H 2S.Preferably X is those compounds of O, and wherein particularly preferred compound is a water.
Other examples of compounds that can be used for treatment step (a) is CO, COS, CS 2, CO 2, O 2With alkyne series or allenic compound.
The compound of tool deactivation and transition metal M IThe catalyzer that mol ratio between the compound preferably wants to guarantee step (A) is inactivation basically.This ratio is preferably greater than 50, more preferably greater than 150, is preferably greater than 250 especially.
Treatment step (a) (wherein the polymkeric substance that makes of these deactivation compounds and step (A) is in contact with one another) can carry out with diverse ways.One of method is that polymkeric substance is contacted with solution, suspension or the dispersion liquid of the varsol of the compound that contains the tool deactivation, and the time can be from 1 minute to several hours.A hexane that example is a humidification of the dispersion liquid of deactivation compounds in varsol.Treatment step (a) is removed liquid after finishing, and makes polymkeric substance carry out treatment step (b).
Preferably use the solution of compound in varsol of transition metal M when carrying out treatment step (b), this solution contains the dissolved alkylaluminium cpd, as triisobutyl aluminium, triethyl aluminum and/or aikyiaiurnirsoxan beta, for example poly-methylaluminoxane (MAO), four isobutyl aluminium alkoxides or four (2,5-dimethyl hexyl)-aikyiaiurnirsoxan beta.The mol ratio of alkylaluminium cpd and transition metal M compound is greater than 2, preferably between 5 and 1000.When carrying out described treatment step (b), can make polymer suspension that step (a) obtains in the varsol of the compound that contains the dissolved transition metal M and optional alkylaluminium cpd and/or aikyiaiurnirsoxan beta, usually service temperature is 0-100 ℃, be preferably 10-60 ℃, processing finishes the back except that desolvating.Perhaps, will be contacted with the compound solution of anhydrous transition metal M by the polymkeric substance that (a) obtains, this solution contains seldom puts solvent so that described compound remains in the solution.Step (B) can be carried out under gas phase in an annular-pipe reactor, and in reactor, the polymkeric substance that the first step polymerization generates circulates under the effect of inert gas.The solution of deactivation compounds and transition metal M compound for example successively is added in the gas phase of annular-pipe reactor with injector, obtains mobile product after processing finishes.Be that in step (b) before, with the compound of product with the energy purification systems, for example alkylaluminium cpd is handled easily.
Amount (in the metal) variation range that is contained in the transition metal M compound in the product that step (B) obtains is very wide, and it depends on the compound of used transition metal M and the relative quantity of the product that needs to prepare in each step.Usually, this amount is 1 * 10 -7-5 * 10 -3G metal M/g product is preferably 5 * 10 -7-5 * 10 -4, more preferably 1 * 10 -6-1 * 10 -4
Second polymerization procedure (C) can carry out in one or several reactor under liquid phase or the gas phase.Liquid phase can be made of (suspension method) inert hydrocarbon solvent, or by one or more alkene CH 2=CHR forms (liquid monomer method).Vapour phase polymerization can be carried out in fluidized-bed reactor or mechanical stirring reactor.During described step (C), normally in polymerization reactor, add the alkylaluminium cpd that is selected from trialkylaluminium, wherein alkyl is the alkyl of 1-12 carbon atom, and contains repeating unit-(R 4) line style or cyclic aluminium alkoxide compound, the wherein R of AlO- 4Be the alkyl of 1-12 carbon atom or the cycloalkyl or the aryl of 6-10 carbon atom, described aluminium alkoxide compound contains 1-50 repeating unit.In general, when processing (b) alkylaluminium cpd useless in the step (B), just alkylaluminium cpd is added in the polymerization procedure (C).
The advantage applies of the inventive method is aspect the handiness two of the quality of the finished product and method.In fact, treatment step (B) makes step (A) might use different catalyst systems with (C).
Particularly, if there is not treatment step (a), the activity for spent catalyst self in the step (A) just needs to generate a large amount of polymkeric substance.But this will cause the product output of described step too big.The result makes in the final product of producing, and will be excessive greatly from the ratio of the product of processing step (A), perhaps produce from step (A) and the unbalanced final product of proportion of products (C), and the size of polymer beads is also improper.
Method of the present invention can be used to prepare the olefin polymer compositions of wide region.Specifically, method of the present invention is particularly suitable for producing high-impact polypropylene (multiphase polymer of propylene).In this case, might obtain not having long same monomeric unit segmental elastocopolymer, so the multipolymer that obtains has useful elasticity.
In fact, the present invention also comprises the method for making of propylene heterophasic copolymer, it is characterized in that it comprises:
(A) first polymerization procedure, wherein perhaps ethene and/or one or more alkene CH of propylene 2=CHR II(R in the formula IIBe the alkyl that contains 2-10 carbon atom) in one or several reactor, containing alkylaluminium cpd, the electronic donor compound capable of choosing any one kind of them (external electronic donor) with contain at least a that be selected from titanium and vanadium and do not contain M IThe transition metal M of-π key ICompound, there is polymerization down in the catalyzer of the solids fraction reaction product of the magnesium halide in active and the electronic donor compound capable (interior electron donor(ED)) of choosing any one kind of them, obtain olefin polymer, the porousness of this polymkeric substance (representing with porosity) is greater than 10%, by ethene and/or CH 2=CHR IIThe unit content that constitutes is less than 20% (weight), and the unit content that is made of propylene is greater than 80% (weight), and the not solubleness in dimethylbenzene is greater than 60%.
(B) treatment step, wherein the product that described step (A) is obtained is with any order:
(a) with can make step (A) in the compound of catalyst deactivation contact;
(b) contact with the compound of the transition metal M that is selected from Ti, Zr, V or Hf that contains at least one M-π key and optional alkylaluminium cpd;
(C) second polymerization procedure, wherein one or more alkene CH 2(R is hydrogen or the alkyl that contains 1-10 carbon atom to=CHR in the formula, cycloalkyl or aryl) polymerization in the presence of the product that in 1 or several reactor, in step (B), obtains, basically be alkene (being total to) polymkeric substance of amorphous, its amount accounts for step (A) and the 20-80% (weight) of the polymkeric substance total amount that (C) generates.
Unit and/or CH that preferably high normal alfon of polymkeric substance that generates in described first polymerization procedure (A) or ethene constitute 2=CHR IIThe unitary content that constitutes is less than the crystalline propylene copolymer of 10% (weight).
The non-limiting instance of alkene (being total to) polymkeric substance of the amorphous basically of step (C) preparation has elastocopolymer and the ethene and the propylene of ethene and propylene and the elasticity terpolymer of a small amount of diolefine, the about 30-70% of unitary content (weight) that therein ethylene constitutes is arranged; Ethene and the elastocopolymer of butylene and the elasticity terpolymer of ethene, butylene and propylene of the about 30-70% of unitary content (weight) that constitutes by ethene; The Atactic Polypropelene of high molecular (η＞1).The example of these multipolymers has been described among European patent application EP-A-586658, EP-A-604917 and disclosures in Italian patent application MI-93A000943, MI-93A001405, MI-93A001406, MI-93A001960 and the MI-93A001963, during with reference to these patents, what relate to is the part of the sign of product and product used catalyzer when preparing.
Polymerization procedure (A) can carry out in one or several annular-pipe reactor in propylene liquid easily, perhaps carries out in one or several fluidized-bed reactor or mechanical stirring reactor in gas phase.Preferably use the vapor phase process of fluidized-bed.
Polymerization procedure (C) is preferably in one or several with carrying out in the Gas-phase reactor of fluidized-bed.Also can be with other method (for example suspension polymerization or with the vapour phase polymerization of mechanical stirring bed).
The porousness (representing with porosity) of the polymkeric substance that first polymerization procedure (A) generates is preferably greater than 15%, more preferably greater than 20%.Pore size distribution is that the aperture of 40% above hole is greater than 10000 .To the polymkeric substance of high porosity, preferably the aperture of 90% above hole is greater than 10000 .
The amount of polymers that polymerization procedure (C) generates account for step (A) and (C) total amount of the polymkeric substance of generation be preferably 25-75%, 35-65% more preferably.
Method of the present invention is preferably carried out continuously, polymerization (A) and (C) two steps in gas-phase fluidized-bed reactor, operate, step (B) is then finished in the gas phase annular-pipe reactor.When carrying out polymerization procedure (A), preferably propylene or itself and ethene and/or CH 2=CHR IIThe polymerization in the presence of the catalyzer described in (A) of the mixture of alkene, monomer consumption are the 5-500g/g catalyzer.
The following examples illustrate the present invention better, but do not limit the present invention.
The performance of pointing out is measured in the following method:
-porosity and nitrogen method surface-area: measure (equipment used: the SORPTOMATIC 1800 of CarloErba company) according to the B.E.T method
-catalyst grain size: by based on the method for the light scattering principle of one-wavelength laser Instrument measuring with " MalvernInstr.2600 ".Mean size is called P50
-melt index E (MIE): measure according to ASTM-D 1238 method E.
-melt index F (MIF): measure according to ASTM-D 1238 method F.
-melt index is than (F/E): the ratio of melt index F and melt index E.
-melt index L (MIL): according to ASTM-D 1238, method L measures.
-flowability: for the 100g polymkeric substance flow through-individual aperture is that 1.25cm and wall and vertical direction are inclined to 20 ° needed time of funnel.
-density: DIN 53194.
The form of-polymer beads and size-grade distribution: ASTM-D 1921-63.-be dissolved in the mark of dimethylbenzene: by polymkeric substance is dissolved in the dimethylbenzene that boils, measures insolubles content after being cooled to 25 ℃ and measure.
-co-monomer content: with the weight percentage of infrared measurement comonomer.
-effective density: ASTM-D 792
-porosity: measure by the method that pressure absorbs mercury down with the porosity that hole percentage ratio is represented.The volume of the mercury that is absorbed promptly is the volume in hole.What this measuring method was used is and mercury reservoir and high vacuum mercury (1 * 10 -2Mba) dilatometer of the demarcation of Xiang Lianing (diameter 3mm) CD3 (Carlo Erba company).The sample (about 0.5g) of weighing is placed dilatometer.Then this device is in high vacuum (＜0.1mmHg) under, and kept with this understanding 10 minutes.Then dilatometer is connected with the mercury reservoir, makes mercury slowly flow to dilatometer, the height shown in dilatometer is 10cm.Close dilatometer and lead to the valve of vacuum pump, with nitrogen (2.5kg/cm 2) to the device pressurization.Under pressure, mercury column has decline in various degree according to material porousness difference.In case the highly stable no longer decline of mercury column in dilatometer, record height value at this moment, the volume in hole can be by equation V=R 2π Δ H obtains, and R is the radius of dilatometer in the formula, and Δ H is the final difference of altitude (in cm) of mercury column initial sum in the dilatometer.Ooze the apparent volume value V of the preceding sample of mercury by dilatometer, dilatometer+mercury, dilatometer+mercury+sample being weighed, can obtaining 1, the volume of sample can be represented by the formula:
V 1=[P 1-(P 2-P)]/the D formula in P be the weight (g) of sample, P 1Be the weight (g) of dilatometer+mercury, P 2Be the weight (g) of dilatometer+mercury+sample, D is that the density of mercury (is 13.546g/cm at 25 ℃ 3).Porosity just can be by formula X=(100V)/V 1Obtain.
-limiting viscosity (IV): in naphthane, measure at 135 ℃.
Embodiment
Embodiment 1 (comparative example)
Step (A): the preparation of PP homopolymer
In the 50ml glass flask, 0.0161g is contacted with 0.31g cyclohexyl methyl dimethoxy silane (CMMS) with 0.799g triethyl aluminum (TEAL) in the 8ml anhydrous hexane in advance by the ingredient of solid catalyst of embodiment 3 preparation of European patent application EP-A-395083.This mixture imported in 4.25 liters the stainless steel still, this stainless steel still passes through purifying treatment in advance, at first uses hexane 80 ℃ of continuous washing 1 hour, and then purges 1 hour at 80 ℃ with propylene steam.Next step imports the 1752g propylene liquid in the still with 982ml hydrogen under 30 ℃.Temperature rises to 70 ℃, carries out polymerization 180 minutes, obtains the following polypropylene of 248g performance: IV=1.55dl/g; Insolubles in the dimethylbenzene=96% (weight).
Step (C): the copolymerization of ethene and propylene
After removing propylene, in above-mentioned same reactor, under 50 ℃ of temperature and 19.5 bar pressures, add the 500g liquid propane gas.Import 7mmol then and be dissolved in M-MAO among the ISOPAR C, allow mixture contact 10 minutes at 50 ℃, remove propane with evaporating down, clean at 50 ℃ with propylene steam again, to remove residual propane at 50 ℃ with polymkeric substance.Under 50 ℃, in the polymkeric substance of the interior gained of above-mentioned reactor, add 19.3g ethene and 41.6g propylene.These two kinds of monomeric mixtures that contain 60% (weight) ethene by importing carry out polymerization.50 ℃ and 9 the crust under carried out copolymerization 120 minutes.Obtain 276g performance multipolymer as shown in table 1.
Embodiment 2 (comparative example)
Step (A): the preparation of PP homopolymer
As described in the steps A of embodiment 1, prepare catalyzer and alfon.Carry out polymerization with the 0.0132g ingredient of solid catalyst, obtain the homopolymer that 209g has following performance: IV=1.57dl/g; Insolubles in the dimethylbenzene=96.1% (weight).
Step (B): use EBTHI-ZrCl 2Handle (b)
After removing propylene 1, under 50 ℃ of temperature and 19.5 bar pressures, in above-mentioned same reactor, add the 500g liquid propane gas.Then 0.005g is contacted 10 minutes EBTHI-ZrCl with the M-MAO of 11.7mmol down in advance at 25 ℃ in ISOPAR C 2Import.Allow mixture contact 10 minutes with polymkeric substance down at 50 ℃.Remove propane with evaporation down at 50 ℃, clean down at 50 ℃ with propylene steam again, to remove residual propane.
Step (C): the copolymerization of ethene and propylene
Carry out copolymerization 240 minutes by the described program of embodiment 1 step (C), obtain 381g performance multipolymer as shown in table 1.
Embodiment 3:
Step (A): the preparation of PP homopolymer
Prepare catalyzer and alfon as the described method of embodiment 1 step (A).Carry out polymerization with the 0.0146g ingredient of solid catalyst, obtain the following homopolymer of 186g performance: IV=1.55dl/g; Insolubles in the dimethylbenzene=95.9% (weight).
Step (B): with water treatment (a) with use EBTHI-ZrCl 2Handle (b)
After the propylene degassing, in above-mentioned same reactor, add 1000ml 0.0513gH 2The hexane of O humidification.Be allowed to condition at 50 ℃ and contact 30 minutes with polymkeric substance down with in the nitrogen atmosphere.With siphonage sucking-off liquid, at room temperature clean by vacuum/logical nitrogen cycle.Under 50 ℃ of temperature and 19.5 bar pressures, the 500g liquid propane gas is added in the described reactor.Import 0.005g then and in ISOPAR C, contact 10 minutes EBTHI-ZrCl in advance with the M-MAO of 11.7mmol down in 25 ℃ 2Allow polymkeric substance contact 10 minutes with this mixture down at 50 ℃.Under 50 ℃, remove propane, clean under 50 ℃ with propylene steam again, to remove residual propane by evaporation.
Step (C): the copolymerization of ethene and propylene
Carry out copolymerization 50 minutes by the described program of embodiment 1 step (C), obtain 256g performance multipolymer as shown in table 1.
Embodiment 4 (comparative example)
Step (A): the preparation of PP homopolymer
In the 50ml glass flask, 0.0187g is contacted with 0.0706g cyclohexyl methyl dimethoxy silane (CMMS) with 1.48g triisobutyl aluminium (TIBAL) in the 8ml anhydrous hexane in advance by the ingredient of solid catalyst of embodiment 3 preparation of European patent application EP-A-395083.This mixture imported in 4.25 liters the stainless steel still, this stainless steel still passes through purifying treatment in advance, at first with hexane 80 ℃ of washings 1 hour, and then with propylene steam 80 ℃ of purgings 1 hour.Under 30 ℃, the 1286g propylene liquid is imported in the still then.Temperature rises to 70 ℃, carries out polymerization 120 minutes, obtains the following homopolymer of 32g performance: IV=5.68dl/g; Insolubles in the dimethylbenzene: 89.7% (weight).
Step (C): the copolymerization of ethene and propylene
After the propylene degassing, under 50 ℃ of temperature and 19.5 bar pressures, in above-mentioned same reactor, add the 500g liquid propane gas.Import 9.38mmol then and be dissolved in the TIBAO of hexanaphthene, allow mixture contact 10 minutes at 50 ℃, under 50 ℃, remove propane, clean at 50 ℃ with propylene steam again, to remove residual propane by evaporation with polymkeric substance.At 50 ℃ of down adding 33.8g ethene and 72.9g propylene in the product of gained in the above-mentioned reactor.Two kinds of monomeric mixtures that contain 60% (weight) ethene by adding make the component of multipolymer keep constant.Copolymerization 50 ℃ and 15 the crust under carried out 245 minutes.Obtain 315g performance multipolymer as shown in table 2.
Embodiment 5 (comparative example)
Step (A): the preparation of PP homopolymer
Catalyzer and alfon are pressed the described method preparation of embodiment 4 steps (A).With
0.02g ingredient of solid catalyst carries out polymerization, obtains the following homopolymer of 69g performance:
IV=4.69dl/g; Insolubles in the dimethylbenzene=82% (weight).
Step (B): use EBTHI-ZrCL 2Handle (b)
After the propylene degassing, under 50 ℃ of temperature and 19.5 bar pressures, in above-mentioned same reactor, add the 500g liquid propane gas.Import 0.004g then and in hexanaphthene, contact 10 minutes EBTHI-ZrCl in advance with the TIBAO of 9.38mmol down in 25 ℃ 2Allow polymkeric substance contact 10 minutes with this mixture, under 50 ℃, remove propane, clean under 50 ℃ with propylene steam again, to remove residual propane by evaporation at 50 ℃.
Step (C): the copolymerization of ethene and propylene
Carry out copolymerization 54 minutes by the described program of embodiment 1 step (C), obtain 353g performance multipolymer as shown in table 2.
Embodiment 6
Step (A): the preparation of PP homopolymer
Catalyzer and alfon are pressed the described method preparation of embodiment 4 steps (A).Carry out polymerization with the 0.0414g ingredient of solid catalyst, obtain the following homopolymer of 170g performance: IV=4.4dl/g; Insolubles 2 85.3% (weight) in the dimethylbenzene.
Step (B): with water treatment (a) with use EBTHI-ZrCl 2Handle (b)
After the propylene degassing, in above-mentioned reactor, add 1000ml 0.068g H 2The hexane of O humidification.Be allowed to condition at 50 ℃ with nitrogen atmosphere in contact 30 minutes with polymkeric substance.With siphonage sucking-off liquid.At room temperature clean by vacuum/logical nitrogen cycle.The TIBAL that 1.48g is dissolved in the 500g liquid propane gas under 50 ℃ of temperature and 19.5 bar pressures is added in the described reactor.Allow polymkeric substance contact 20 minutes at 50 ℃ with this mixture.Import 0.020g then and in hexane, contact 10 minutes EBTHI-ZrCl in advance with 46.9mmol TIBAO down in 25 ℃ 2Allow polymkeric substance contact 10 minutes at 50 ℃ with this mixture.Under 50 ℃, remove propane, clean under 50 ℃ with propylene steam again, to remove residual propane by evaporation.
Step (C): the copolymerization of ethene and propylene
Carry out copolymerization 81 minutes by the described method of embodiment 1 step (C), obtain 260g performance multipolymer as shown in table 2.
Table 1
The performance of the multipolymer of embodiment 1-3
Embodiment ???1 ???2 ??????3
EPR % (weight) ?21.4 ?53.8 ????40.2
M.p.DSC * ℃ ?118 ?116 ?????--
M.p.DSC * ℃ ?167 ?164 ????166
Xylene soluble part % (weight) ?12.9 ?43.9 ????42
The dimethylbenzene insolubles % (weight) ?87.1 ?56.1 ????58
The IV homopolymer dl/g ?1.55 ?1.57 ????1.55
The IV final product dl/g ?2.77 ?2.71 ????1.24
Table 2
The performance of the multipolymer of embodiment 4-6
Embodiment No. ??4 ?????5 ?????6
EPR % (weight) ?90 ????82 ????35
M.p.DSC * ℃ ?116 ????113 ????--
M.p.DSC * ℃ ?158 ????156 ????159
Xylene soluble part % (weight) ?53.2 ????58.4 ????41.1
The dimethylbenzene insolubles % (weight) ?44.7 ????39.8 ????57.9
The IV homopolymer dl/g ?5.68 ????4.69 ????4.4
The IV final product dl/g ?8.81 ????6.35 ????2.96
*Observe 100-180 ℃ of section of differential thermogram, the fusing point peak may appear in the hypocrystalline part (as the words that generate) of PP homopolymer and rubber in this zone.

Claims (24)

1. one or more general formulas CH 2The multistep polymerization method of the alkene the shown in=CHR (wherein R is hydrogen or alkyl, cycloalkyl or the aryl that contains 1-10 carbon atom) is characterized in that it comprises:
(A) the first step polymerization, wherein one or more described alkene CH 2=CHR aggregates into olefin homo or multipolymer in one or several reactor in the presence of catalyzer, described catalyzer contains alkylaluminium cpd and the transition metal M that is selected from Ti and V that contains no M-π key ICompound and the reaction product between the solids component of magnesium halide in active;
(B) treatment step, wherein the product that first polymerization procedure (A) is obtained is with any order:
(a) contact with the compound that can make the middle catalyst deactivation that exists of described step (A);
(b) contact with optional alkylaluminium cpd with the compound of the filtering metal M that is selected from Ti, Zr, V or Hf that contains at least one M-π key;
(C) the second step polymerization, wherein one or more described alkene carry out polymerization in one or several reactor in the presence of the product that described treatment step obtains.
2. in accordance with the method for claim 1, wherein step (A) olefin homo that is generated or the porosity of multipolymer are represented with hole percentage ratio, greater than 5%.
3. in accordance with the method for claim 2, wherein step (A) olefin homo that is generated or the porosity of multipolymer are represented with hole percentage ratio, greater than 10%.
4. in accordance with the method for claim 1, wherein magnesium halide in active is MgCl 2, transition metal M ICompound be selected from: the halogen alcoholate of halogenated titanium, Ti, VCl 3, VCl 4, VOCl 3, V the halogen alcoholate.
5. in accordance with the method for claim 4, wherein the Ti compound is selected from: TiCl 4, TiCl 3With formula Ti (OR I) mX nThe halogen alcoholate, R in the formula IBe contain 1-12 carbon atom alkyl or-COR IGroup, X are halogens, (m+n) are the valence mumbers of Ti.
6. in accordance with the method for claim 1, wherein the used solid ingredient of first polymerization procedure (A) is that mean diameter is the spheroidal particle of 10-150 μ m.
7. in accordance with the method for claim 1, wherein transition metal M contains the ligand L of at least one and metal-complexing, and described ligand L has monocycle or the polynuclear plane that contains conjugated pi electron.
8. in accordance with the method for claim 7, wherein the compound of transition metal M is selected from:
Cp IMR 1 aR 2 bR 3 c???????(I)
Cp IC p IIMR 1 aR 2 b??????(II)
(Cp 1-A e-Cp II) MR 1 aR 2 b(III) wherein M is Ti, V, Zr and Hf; Cp IAnd Cp IICan be identical or different, can be the cyclopentadienyl group of cyclopentadienyl group or replacement; Two or more substituting groups on described cyclopentadienyl group can form the ring of one or more 4-6 of containing carbon atom; R 1, R 2And R 3Can be identical or inequality, can be hydrogen atom, halogen, contain alkyl or alkoxyl group, aryl, the alkaryl that contains 6-20 carbon atom or the aralkyl of 1-20 carbon atom, contain acyloxy, the allyl group of 1-20 carbon atom, the substituting group of silicon atoms; A is alkenyl bridge or is selected from the group with following array structure:
Figure A9519144400031
=AlR 1,-Ge-,-Sn-,-O-,-S-,=SO ,=SO 2,=NR 1,=PR 1,=P (O) R 1, M wherein 1Be Si, Ge or Sn; R 1And R 2Can be identical or inequality, can be the alkyl that contains 1-4 carbon atom or contain the aryl of 6-10 carbon atom; A, b, c are the integer of 0-4 independently; E is the integer of 1-6, two or several R 1, R 2And R 3Group can form a ring.
9. in accordance with the method for claim 7, wherein transistion metal compound is selected from the compound with following array structure: (Me 5Cp) MMe 3, (Me 5Cp) M (OMe) 3, (Me 5Cp) MCl 3, (Cp) MCl 3, (Cp) MMe 3, (MeCp) MMe 3, (Me 3Cp) MMe 3, (Me 4Cp) MCl 3, (Ind) MBenz 3, (H 4Ind) MBenz 3, (Cp) MBu 3
10. in accordance with the method for claim 7, wherein transistion metal compound is selected from the compound with following array structure: (Cp) 2MMe 2, (Cp) 2MPh 2, (Cp) 2MEt 2, (Cp) 2MCl 2, (Cp) 2M (OMe) 2, (Cp) 2M (OMe) Cl, (MeCp) 2MCl 2, (Me 5Cp) 2MCl 2, (Me 5Cp) 2MMe 2, (Me 5Cp) 2MMeCl, (Cp) (Me 5Cp) MCl 2, (1-MeFlu) 2MCl 2, (BuCp) 2MCl 2, (Me 3Cp) 2MCl 2, (Me 4Cp) 2MCl 2, (Me 5Cp) 2M (OMe) 2, (Me 5Cp) 2M (OH) Cl, (Me 5Cp) 2M (OH) 2, (Me 5Cp) 2M (C 6H 5) 2, (Me 5Cp) 2M (CH 3) Cl, (EtMe 4Cp) 2- 2MCl 2, [(C 6H 5) Me 4Cp] 2MCl 2, (Et 5Cp) 2MCl 2, (Me 5Cp) 2-M (C 6H 5) Cl, (Ind) 2MCl 2, (Ind) 2MMe 2, (H 4Ind) 2MCl 2, (H 4Ind) 2MMe 2, { [Si (CH 3) 3] Cp} 2MCl 2, { [Si (CH 3) 3] 2Cp} 2MCl 2, (Me 4Cp) (Me 5Cp) MCl 2
11. in accordance with the method for claim 7, Qi Zhong transistion metal compound Xuan Zi has the compound of Xia array structure: C2H 4(Ind) 2MCl 2，C 2H 4(Ind) 2MMe 2，C 2H 4(H 4Ind) 2MCl 2， C 2H 4(H 4Ind) 2MMe 2，Me 2Si(Me 4Cp) 2MCl 2，Me 2Si(Me 4Cp) 2MMe 2， Me 2SiCp 2MCl 2，Me 2SiCp 2MMe 2，Me 2Si(Me 4Cp) 2MMeOMe，Me 2Si(Flu) 2-MCl 2， Me 2Si(2-Et-5-iPrCp) 2MCl 2，Me 2Si(H 4Ind) 2MCl 2， Me 2Si-(H 4Flu) 2MCl 2，Me 2SiCH 2(Ind) 2MCl 2，Me 2Si(2-Me-H 4Ind) 2MCl 2， Me 2Si(2-MeInd) 2MCl 2，Me 2Si(2-Et-5-iPr-Cp) 2MCl 2，Me 2Si(2-Me-5-EtCp) 2MCl 2， Me 2Si(2-Me-5-Me-Cp) 2MCl 2，Me 2Si (2-Me-4,5-benzindene base)2MCl 2，Me 2Si (4,5-benzindene base)2MCl 2，Me 2Si(2-EtInd) 2MCl 2， Me 2Si(2-iPr-Ind) 2MCl 2，Me 2Si (the MCl of 2-Shu butyl-Ind)2，Me 2Si (3-Shu butyl-5-MeCp)2MCl 2，Me 2Si (3-Shu butyl-5-MeCp)2MMe 2，Me 2Si(2-MeInd) 2MCl 2，C 2H 4(2-Me-4,5-benzindene base)2MCl 2，Me 2C(Flu)CpMCl 2，Ph 2Si(Ind) 2MCl 2， Ph(Me)Si(Ind) 2MCl 2，C 2H 4(H 4Ind)M(NMe 2) OMe, isopropylidene-((Flu) MCl of 3-Shu butyl-Cp)2，Me 2C(Me 4Cp)(MeCp)MCl 2， MeSi(Ind) 2MCl 2，Me 2Si(Ind) 2MMe 2，Me 2Si(Me 4Cp) 2MCl(OEt)， C 2H 4(Ind) 2M(NMe 2) 2，C 2H 4(Me 4Cp) 2MCl 2，C 2Me 4(Ind) 2MCl 2， Me 2Si(3-Me-Ind) 2MCl 2，C 2H 4(2-Me-Ind) 2MCl 2，C 2H 4(3-Me- Ind) 2 MCl 2 ，C 2H 4(4，7-Me 2-Ind) 2MCl 2，C 2H 4(5，6-Me 2-Ind) 2MCl 2, C 2H 4(2，4，7-Me 3Ind) 2MCl 2，C 2H 4(3，4，7-Me 3Ind) 2MCl 2， C 2H 4(2-Me-H 4Ind) 2MCl 2，C 2H 4(4，7-Me 2-H 4Ind) 2MCl 2， C 2H 4(2，4，7-Me 3-H 4Ind) 2-MCl 2，Me 2Si(4，7-Me 2-Ind) 2MCl 2， Me 2Si(5，6-Me 2-Ind) 2MCl 2，Me 2Si(2，4，7-Me 3-H 4Ind) 2MCl 2。
12. in accordance with the method for claim 1, wherein used catalyzer contains alkylaluminium cpd, is selected from Ti and V with containing for electron compound (external electronic donor) in first polymerization procedure (A), and does not contain M IThe transition metal M of-π key ICompound, magnesium halide in active and give reaction product between the solid ingredient of electron compound (interior electron donor(ED)).
13. in accordance with the method for claim 12, be selected from general formula R wherein for electron compound (external electronic donor) 1R 2Si (OR) 2Silicon compound, R in the formula 1And R 2Can be identical or different, can be alkyl, cycloalkyl or the aryl of 1-18 carbon atom, R is the alkyl of 1-4 carbon atom.
14. in accordance with the method for claim 1, the compound of catalyst system therefor inactivation in the step (A) is selected from: CO, COS, CS 2, CO 2, O 2, alkyne series compound, allenic compound and general formula be R Y-1The compound of XH, R is hydrogen or the alkyl that contains 1-10 carbon atom in the formula, and X is O, N or S, and y is the valence mumber of X.
15. in accordance with the method for claim 1, wherein can make the compound of the catalyst deactivation of step (A) is water.
16. the product that wherein in step (B), first polymerization procedure (A) is obtained in accordance with the method for claim 1:
(a) contact this compound and M with solution, suspension or the dispersion liquid of the aliphatic hydrocarbon solvent of the compound that contains the tool deactivation IMol ratio greater than 50; With
(b) use solution-treated, this solution contain transition metal M compound and be selected from trialkylaluminium, wherein alkyl has 1-12 carbon atom, alkylaluminium cpd and contain repeating unit-(R 4) AlO-(R in the formula 4Be the alkyl of 1-12 carbon atom or the cycloalkyl or the aryl of 6-10 carbon atom) line style or ring-type aluminium alkoxide compound, described aluminium alkoxide compound contains 1-50 repeating unit.
17. in accordance with the method for claim 1, wherein during polymerization procedure (C), have at least a reactor will add the product that treatment step (B) obtains and add at the same time or separately and be selected from trialkylaluminium, wherein alkyl has 1-12 carbon atom, alkylaluminium cpd and contain repeating unit-(R 4) AlO-(R in the formula 4Be the alkyl of 1-12 carbon atom or the cycloalkyl or the aryl of 6-10 carbon atom) line style or ring-type aluminium alkoxide compound, described aluminium alkoxide compound contains 1-50 repeating unit.
18. in accordance with the method for claim 1, wherein polymerization procedure (A) carries out in liquid phase, and described liquid phase is by hydrocarbon solvent or one or more alkene CH 2=CHR forms; And wherein polymerization procedure (C) carries out in the Gas-phase reactor of at least one fluidized-bed or mechanical stirring bed.
19. in accordance with the method for claim 1, wherein step (A) and polymerization (C) are all carried out in the Gas-phase reactor of fluidized-bed or mechanical stirring bed.
20. in accordance with the method for claim 1, wherein treatment step (B) carries out in the gas phase annular-pipe reactor.
21. in accordance with the method for claim 1, wherein the amount of the polymkeric substance that generated of step (A) accounts for step (A) and the 10-90% (weight) of the total amount of the polymkeric substance that (C) generated.
22. in accordance with the method for claim 1, wherein the amount of the polymkeric substance that generated of step (A) accounts for step (A) and the 20-80% (weight) of the total amount of the polymkeric substance that (C) generated.
23. a multistep processes for preparing the propylene heterophasic copolymer is characterized in that it comprises:
(A) first polymerization procedure, wherein perhaps ethene and/or one or more alkene CH of propylene 2=CHR II(R in the formula IIBe the alkyl that contains 2-10 carbon atom) in one or several reactor, containing alkylaluminium cpd, the electronic donor compound capable of choosing any one kind of them (external electronic donor) with contain at least a that be selected from titanium and vanadium and do not contain M IThe transition metal M of-π key ICompound, there is polymerization down in the catalyzer of the solids fraction reaction product of the magnesium halide in active and the electronic donor compound capable (interior electron donor(ED)) of choosing any one kind of them, obtain olefin polymer, the porousness of this polymkeric substance (representing with porosity) is greater than 10%, by ethene and/or CH 2=CHR IIThe unit content that constitutes is less than 20% (weight), and the unit content that is made of propylene is greater than 80% (weight), and the not solubleness in dimethylbenzene is greater than 60%;
(B) treatment step, wherein the product that described step (A) is obtained is with any order:
(a) with can make step (A) in the compound of catalyst deactivation contact;
(b) contact with the compound of the transition metal M that is selected from Ti, Zr, V or Hf that contains at least one M-π key and optional alkylaluminium cpd;
(C) second polymerization procedure, wherein one or more alkene CH 2(R is hydrogen or the alkyl that contains 1-10 carbon atom to=CHR in the formula, cycloalkyl or aryl) polymerization in the presence of the product that in 1 or several reactor, in step (B), obtains, basically be alkene (being total to) polymkeric substance of amorphous, its amount accounts for step (A) and the 20-80% (weight) of the polymkeric substance total amount that (C) generates.
24. the olefin homo or the multipolymer that obtain according to claim 1 or 23 described methods.
CN95191444A 1994-10-05 1995-10-02 Process for the (co) polymerization of olefins Expired - Fee Related CN1070505C (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI94A002028 1994-10-05
ITMI942028A IT1270125B (en) 1994-10-05 1994-10-05 PROCESS FOR THE (CO) POLYMERIZATION OF OLEFINE

Publications (2)

Publication Number Publication Date
CN1139934A true CN1139934A (en) 1997-01-08
CN1070505C CN1070505C (en) 2001-09-05

Family

ID=11369652

Family Applications (1)

Application Number Title Priority Date Filing Date
CN95191444A Expired - Fee Related CN1070505C (en) 1994-10-05 1995-10-02 Process for the (co) polymerization of olefins

Country Status (29)

Country Link
US (2) US5648422A (en)
EP (1) EP0742801B1 (en)
JP (1) JP3897359B2 (en)
KR (1) KR100399625B1 (en)
CN (1) CN1070505C (en)
AT (1) ATE200499T1 (en)
AU (1) AU694276B2 (en)
BG (1) BG100674A (en)
BR (1) BR9506402A (en)
CA (1) CA2178077A1 (en)
CZ (1) CZ287739B6 (en)
DE (1) DE69520662T2 (en)
DK (1) DK0742801T3 (en)
ES (1) ES2156948T3 (en)
FI (1) FI962329A0 (en)
GR (1) GR3035745T3 (en)
HU (1) HU216285B (en)
IL (1) IL115515A (en)
IT (1) IT1270125B (en)
MY (1) MY112181A (en)
NO (1) NO311179B1 (en)
PH (1) PH31450A (en)
PL (1) PL314853A1 (en)
PT (1) PT742801E (en)
RU (1) RU2171265C2 (en)
SK (1) SK281619B6 (en)
TR (1) TR199501214A2 (en)
WO (1) WO1996011218A1 (en)
ZA (1) ZA958316B (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101331164B (en) * 2005-09-15 2011-03-23 陶氏环球技术公司 Control of polymer architecture and molecular weight distribution via multi-centered shuttling agent
CN104341544A (en) * 2013-08-09 2015-02-11 切弗朗菲利浦化学公司 Methods for controlling dual catalyst olefin polymerizations with an alcohol compound
CN105254808A (en) * 2015-09-30 2016-01-20 宁波职业技术学院 Method for preparing modified petroleum resin
CN105622808A (en) * 2014-10-31 2016-06-01 中国石油化工股份有限公司 Method for producing impact-resistant polypropylene
CN107667139A (en) * 2015-06-05 2018-02-06 埃克森美孚化学专利公司 Heterophasic copolymer and sequential polymerization
CN110551242A (en) * 2018-05-31 2019-12-10 中国石油天然气股份有限公司 Impact-resistant co-polypropylene and preparation method thereof

Families Citing this family (53)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1274469B (en) † 1995-05-11 1997-07-17 Spherilene Spa DYNAMICALLY VULCANIZABLE POLYOLEFINIC COMPOSITIONS
AU731426B2 (en) * 1996-06-24 2001-03-29 Montell North America Inc. High transparency and high flexibility elastoplastic polyolefin compositions
ES2198098T3 (en) * 1998-03-09 2004-01-16 Basell Poliolefine Italia S.P.A. MULTIETAPE PROCEDURE FOR POLYMERIZATION OF OLEFINS.
EP0942011B1 (en) * 1998-03-09 2003-05-14 Basell Poliolefine Italia S.p.A. Multi-stage process for the polymerization of olefins
US6268062B1 (en) 1998-04-06 2001-07-31 Applied Extrusion Technologies, Inc. Polypropylene blends and films prepared therewith
US6037417A (en) * 1998-08-18 2000-03-14 Montell Technology Company Bv Polypropylene composition useful for making solid state oriented film
IT1302029B1 (en) 1998-08-19 2000-07-20 Montech Usa Inc PROCESS TO PRODUCE HETEROPHASIC POLYMER COMPOSITIONS AND ECOMPOSITIONS SO OBTAINED
DE60006082T2 (en) * 1999-03-09 2004-07-22 Basell Polyolefine Gmbh MULTI-STAGE PROCESS FOR (CO) POLYMERSATION OF OLEFINS
FI991015A0 (en) * 1999-05-04 1999-05-04 Borealis As Process for the preparation of alpha-olefin polymers
EP1157046B1 (en) 1999-12-28 2005-12-07 Basell Polyolefine GmbH Process for the preparation of ethylene polymers
PL353055A1 (en) 2000-03-22 2003-10-06 Basell Technology Company B.V. Thermoplastic compositions of isotactic propylene polymers and flexible propylene polymers having reduced isotacticity and a process for the preparation thereof
GB0008690D0 (en) * 2000-04-07 2000-05-31 Borealis Polymers Oy Process
AU2001276867A1 (en) * 2000-07-11 2002-01-21 Sri International Encoding methods using up-converting phosphors for high-throughput screening of catalysts
US6673869B2 (en) 2000-07-27 2004-01-06 Basell Poliolefine Italia S.P.A. Transparent elastomeric thermoplastic polyolefin compositions
WO2002051887A2 (en) * 2000-12-22 2002-07-04 Basell Poliolefine Italia S.P.A. Process for the preparation of porous polymers and polymers obtainable thereof
WO2002060957A2 (en) * 2001-01-16 2002-08-08 Exxonmobil Chemical Patents Inc. Catalysts with at least two transition metal compounds and polymerization processes using them
US7365137B2 (en) 2001-07-17 2008-04-29 Basell Polyolefine Gmbh Multistep process for the (co) polymerization of olefins
US20050003951A1 (en) * 2001-11-27 2005-01-06 Angelo Ferraro Porous polymers of propylene
EP1448624A1 (en) * 2001-11-27 2004-08-25 Basell Polyolefine GmbH Process for the treatment of polymer compositions
WO2003059963A1 (en) * 2002-01-15 2003-07-24 Advanced Elastomer Systems, L.P. Thermoplastic elastomers and process for making the same
US7816452B2 (en) * 2002-07-24 2010-10-19 Basell Poliolifine Italia s.r.l. At least two-stage process for preparing propylene polymer compositions
US6833416B2 (en) * 2003-03-21 2004-12-21 Univation Technologies, Llc Methods of polymerizing olefin monomers with mixed catalyst systems
TW200504093A (en) * 2003-05-12 2005-02-01 Dow Global Technologies Inc Polymer composition and process to manufacture high molecular weight-high density polyethylene and film therefrom
CN100594878C (en) * 2004-03-31 2010-03-24 信越化学工业株式会社 Cosmetic containing siloxane polymer
EP1802699B1 (en) * 2004-10-13 2011-07-27 ExxonMobil Chemical Patents Inc. Elastomeric reactor blend compositions
CN1328310C (en) * 2004-11-05 2007-07-25 中国科学院化学研究所 Polyolefin composite material and preparation method
US7629422B2 (en) * 2004-12-21 2009-12-08 Univation Technologies, Llc Process for transitioning between Ziegler-Natta-based and chromium-based catalysts
US20080312390A1 (en) * 2007-06-14 2008-12-18 Petrochina Company Limited Process for preparation of polyolefin alloy
KR101141494B1 (en) * 2007-09-05 2012-05-03 에스케이이노베이션 주식회사 Ethylene copolymer having multiple pitch in molecular weight distribution and the method of preparing the same
MX2011001970A (en) * 2008-08-21 2011-08-12 Dow Global Technologies Llc Catalyst composition with mixed selectivity control agent and polymerisation method using it.
TWI758885B (en) 2010-07-30 2022-03-21 瑞士商愛爾康公司 Hydrated contact lens
ES2605429T3 (en) 2011-06-15 2017-03-14 Borealis Ag Mixing the in situ reactor of a nucleated polypropylene catalyzed by Ziegler-Natta and a metallocene catalyzed polypropylene
EP3083216B1 (en) 2013-12-17 2018-01-31 Novartis AG A silicone hydrogel lens with a crosslinked hydrophilic coating
WO2016032926A1 (en) 2014-08-26 2016-03-03 Novartis Ag Method for applying stable coating on silicone hydrogel contact lenses
US10294316B2 (en) 2015-06-05 2019-05-21 Exxonmobil Chemical Patents Inc. Silica supports with high aluminoxane loading capability
EP3303417A4 (en) * 2015-06-05 2018-08-22 ExxonMobil Chemical Patents Inc. Porous propylene polymers
US10280233B2 (en) 2015-06-05 2019-05-07 Exxonmobil Chemical Patents Inc. Catalyst systems and methods of making and using the same
US9725537B2 (en) 2015-06-05 2017-08-08 Exxonmobil Chemical Patents Inc. High activity catalyst supportation
EP3303418A4 (en) * 2015-06-05 2018-06-20 ExxonMobil Chemical Patents Inc. Bimodal propylene polymers and sequential polymerization
US9725569B2 (en) 2015-06-05 2017-08-08 Exxonmobil Chemical Patents Inc. Porous propylene polymers
CN107922537B (en) 2015-06-05 2021-07-27 埃克森美孚化学专利公司 Preparation of multiphase polymers in gas or slurry phase
WO2016196331A1 (en) 2015-06-05 2016-12-08 Exxonmobil Chemical Patents Inc. Supported metallocene catalyst systems for polymerization
US10280235B2 (en) 2015-06-05 2019-05-07 Exxonmobil Chemical Patents Inc. Catalyst system containing high surface area supports and sequential polymerization to produce heterophasic polymers
US9809664B2 (en) 2015-06-05 2017-11-07 Exxonmobil Chemical Patents Inc. Bimodal propylene polymers and sequential polymerization
CN107690441A (en) 2015-06-05 2018-02-13 埃克森美孚化学专利公司 It is prepared by single reactor of the polymer in gas phase or slurry phase
US9920176B2 (en) 2015-06-05 2018-03-20 Exxonmobil Chemical Patents Inc. Single site catalyst supportation
US9738779B2 (en) 2015-06-05 2017-08-22 Exxonmobil Chemical Patents Inc. Heterophasic copolymers and sequential polymerization
US10329360B2 (en) 2015-06-05 2019-06-25 Exxonmobil Chemical Patents Inc. Catalyst system comprising supported alumoxane and unsupported alumoxane particles
US10077325B2 (en) 2015-06-05 2018-09-18 Exxonmobil Chemical Patents Inc. Silica supports with high aluminoxane loading capability
KR102604468B1 (en) 2015-12-15 2023-11-22 알콘 인코포레이티드 Method for applying stable coatings on silicone hydrogel contact lenses
WO2017204830A1 (en) 2016-05-27 2017-11-30 Exxonmobil Chemical Patents, Inc. Metallocene catalyst compositions and polymerization process therewith
WO2019116141A1 (en) 2017-12-13 2019-06-20 Novartis Ag Method for producing mps-compatible water gradient contact lenses
WO2022106710A1 (en) 2020-11-23 2022-05-27 Borealis Ag In-situ reactor blend of ziegler-natta catalysed, nucleated polypropylene and a metallocene catalysed polypropylene

Family Cites Families (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL162661B (en) * 1968-11-21 1980-01-15 Montedison Spa PROCESS FOR PREPARING A CATALYST FOR THE POLYMERIZATION OF OLEFINS-1.
YU35844B (en) * 1968-11-25 1981-08-31 Montedison Spa Process for obtaining catalysts for the polymerization of olefines
IT1140221B (en) * 1981-10-14 1986-09-24 Montedison Spa POLYPROPYLENE COMPOSITIONS WITH IMPROVED CHARACTERISTICS OF IMPACT RESISTANCE AT LOW TEMPERATURES AND PREPARATION PROCEDURE
US4431571A (en) * 1982-05-14 1984-02-14 Standard Oil Company (Indiana) Retreating comminuted olefin polymerization catalyst with a titanium(IV) compound, a haloalkylchlorosilane and an ester
IT1206128B (en) * 1984-07-30 1989-04-14 Himont Inc IMPACT RESISTANT POLYPROPYLENE COMPOSITIONS WITH IMPROVED WHITENING RESISTANCE.
CA1235543A (en) * 1984-09-12 1988-04-19 Norio Kashiwa Process for producing propylene block copolymer
KR920000173B1 (en) * 1986-10-09 1992-01-09 미쓰이세끼유 가가꾸고오교오 가부시끼가이샤 Low crystal propyrene random copolymer composition and its making method and polypropylene composite lamination
IT1227259B (en) * 1988-09-30 1991-03-28 Himont Inc CATALYSTS FOR THE POLYMERIZATION OF OLEFINE.
IT1227260B (en) * 1988-09-30 1991-03-28 Himont Inc DIETTERS THAT CAN BE USED IN THE PREPARATION OF ZIEGLER-NATTA CATALYSTS
IT1227258B (en) * 1988-09-30 1991-03-28 Himont Inc COMPONENTS AND CATALYSTS FOR THE POLYMERIZATION OF OLEFINE
IT1230134B (en) * 1989-04-28 1991-10-14 Himont Inc COMPONENTS AND CATALYSTS FOR THE POLYMERIZATION OF OLEFINE.
US5280074A (en) * 1989-12-21 1994-01-18 Hoechst Ag Process for the preparation of a polypropylene molding composition
DE3942363A1 (en) * 1989-12-21 1991-06-27 Hoechst Ag METHOD FOR PRODUCING A POLYPROPYLENE MOLDING MATERIAL
DE3942364A1 (en) * 1989-12-21 1991-06-27 Hoechst Ag METHOD FOR PRODUCING A POLYPROPYLENE MOLDING MATERIAL
DE4005947A1 (en) * 1990-02-26 1991-08-29 Basf Ag SOLUBLE CATALYST SYSTEMS FOR POLYMERIZING C (DOWN ARROW) 2 (DOWN ARROW) - TO C (DOWN ARROW) 1 (DOWN ARROW) (DOWN ARROW) 0 (DOWN ARROW) -ALK-1-ENEN
IT1241093B (en) * 1990-03-30 1993-12-29 Himont Inc COMPONENTS AND CATALYSTS FOR THE POLYMERIZATION OF OLEFINE
ES2162953T3 (en) * 1990-11-12 2002-01-16 Basell Polyolefine Gmbh PROCEDURE FOR OBTAINING AN OLEFINE POLYMER.
EP0485822B1 (en) * 1990-11-12 1996-07-03 Hoechst Aktiengesellschaft Process for preparing high molecular weight polyolefines
FR2669915B1 (en) * 1990-11-29 1993-01-29 Atochem MAGNESIUM CHLORIDE PARTICLES WITH POLYHEDRAL STRUCTURE, CATALYTIC COMPONENT SUPPORTED ON THESE PARTICLES, METHODS OF MANUFACTURING THESE PRODUCTS AND POLYOLEFINS OBTAINED FROM THIS CATALYTIC COMPONENT.
EP0527589B1 (en) * 1991-08-08 1998-06-03 Ube Rexene Corporation Resin composition comprising amorphous polyolefin and crystalline polypropylene
DE4130429A1 (en) * 1991-09-13 1993-03-18 Basf Ag METHOD FOR PRODUCING MULTI-PHASE BLOCK COPOLYMERISATS BASED ON ALK-1-ENEN
ES2093166T3 (en) * 1991-11-30 1996-12-16 Hoechst Ag METALOCHENES WITH INDENYL DERIVATIVES CONDENSED WITH BENZO AS LIGANDS, PROCEDURE FOR THEIR PREPARATION AND USE AS CATALYSTS.
IT1262935B (en) * 1992-01-31 1996-07-22 Montecatini Tecnologie Srl COMPONENTS AND CATALYSTS FOR THE POLYMERIZATION OF OLEFINE
IT1262934B (en) * 1992-01-31 1996-07-22 Montecatini Tecnologie Srl COMPONENTS AND CATALYSTS FOR THE POLYMERIZATION OF OLEFINE
DE4206367A1 (en) * 1992-02-29 1993-09-02 Basf Ag METHOD FOR THE PRODUCTION OF PROPYLENE-ETHYLENE COPOLYMERISATS
IT1254547B (en) * 1992-03-23 1995-09-25 Montecatini Tecnologie Srl ELASTOMERIC COPOLYMERS OF ETHYLENE WITH ALPHA-OLEPHINS.
IT1264406B1 (en) * 1993-05-11 1996-09-23 Spherilene Srl AMORPHOUS COPOLYMERS OF ETHYLENE WITH ALPHA-OLEFINS AND PROCEDURE FOR THEIR PREPARATION
DE69307472T2 (en) * 1992-11-10 1997-05-15 Mitsubishi Chem Corp Process for the preparation of alpha-olefin polymers
IT1256260B (en) * 1992-12-30 1995-11-29 Montecatini Tecnologie Srl ATACTIC POLYPROPYLENE
CA2153978C (en) * 1993-01-29 2005-07-12 Brian W. S. Kolthammer Ethylene interpolymerizations
IT1264482B1 (en) * 1993-06-30 1996-09-23 Spherilene Srl AMORPHOUS COPOLYMERS OF ETHYLENE WITH PROPYLENE AND PROCEDURE FOR THEIR PREPARATION
IT1264483B1 (en) * 1993-06-30 1996-09-23 Spherilene Srl ELASTOMERIC COPOLYMERS OF ETHYLENE WITH PROPYLENE
IT1271407B (en) * 1993-09-13 1997-05-28 Spherilene Srl PROCEDURE FOR THE PREPARATION OF ELASTOMERIC ETHYLENE COPOLYMERS AND OBTAINED PRODUCTS
IT1271406B (en) * 1993-09-13 1997-05-28 Spherilene Srl PROCEDURE FOR THE PREPARATION OF ETHYLENE POLYMERS AND OBTAINED PRODUCTS
US5397843A (en) * 1993-11-22 1995-03-14 Igi Baychem, Inc. Polymer compositions comprising amorphous propylene polymer

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101331164B (en) * 2005-09-15 2011-03-23 陶氏环球技术公司 Control of polymer architecture and molecular weight distribution via multi-centered shuttling agent
CN104341544A (en) * 2013-08-09 2015-02-11 切弗朗菲利浦化学公司 Methods for controlling dual catalyst olefin polymerizations with an alcohol compound
CN104341544B (en) * 2013-08-09 2018-06-08 切弗朗菲利浦化学公司 For controlling the method with the bifunctional catalyst olefinic polyreaction of alcoholic compound
CN105622808A (en) * 2014-10-31 2016-06-01 中国石油化工股份有限公司 Method for producing impact-resistant polypropylene
CN105622808B (en) * 2014-10-31 2018-06-15 中国石油化工股份有限公司 A kind of production method of impact polypropylene
CN107667139A (en) * 2015-06-05 2018-02-06 埃克森美孚化学专利公司 Heterophasic copolymer and sequential polymerization
CN105254808A (en) * 2015-09-30 2016-01-20 宁波职业技术学院 Method for preparing modified petroleum resin
CN110551242A (en) * 2018-05-31 2019-12-10 中国石油天然气股份有限公司 Impact-resistant co-polypropylene and preparation method thereof
CN110551242B (en) * 2018-05-31 2022-03-29 中国石油天然气股份有限公司 Impact-resistant co-polypropylene and preparation method thereof

Also Published As

Publication number Publication date
ZA958316B (en) 1996-04-26
FI962329A (en) 1996-06-04
CN1070505C (en) 2001-09-05
RU2171265C2 (en) 2001-07-27
BR9506402A (en) 1997-09-09
PL314853A1 (en) 1996-09-30
IL115515A (en) 2000-07-26
CZ287739B6 (en) 2001-01-17
DE69520662D1 (en) 2001-05-17
MY112181A (en) 2001-04-30
CA2178077A1 (en) 1996-04-18
DK0742801T3 (en) 2001-05-21
ITMI942028A1 (en) 1996-04-05
HU9601834D0 (en) 1996-09-30
AU694276B2 (en) 1998-07-16
US5648422A (en) 1997-07-15
JPH09506391A (en) 1997-06-24
JP3897359B2 (en) 2007-03-22
TR199501214A2 (en) 1996-06-21
ES2156948T3 (en) 2001-08-01
WO1996011218A1 (en) 1996-04-18
ATE200499T1 (en) 2001-04-15
HUT75175A (en) 1997-04-28
PT742801E (en) 2001-08-30
BG100674A (en) 1997-03-31
SK281619B6 (en) 2001-05-10
NO311179B1 (en) 2001-10-22
NO962298D0 (en) 1996-06-04
IL115515A0 (en) 1996-01-19
ITMI942028A0 (en) 1994-10-05
HU216285B (en) 1999-06-28
IT1270125B (en) 1997-04-28
DE69520662T2 (en) 2001-10-18
FI962329A0 (en) 1996-06-04
GR3035745T3 (en) 2001-07-31
CZ199496A3 (en) 1996-12-11
EP0742801B1 (en) 2001-04-11
PH31450A (en) 1998-11-03
EP0742801A1 (en) 1996-11-20
AU3803395A (en) 1996-05-02
NO962298L (en) 1996-06-04
US6028140A (en) 2000-02-22
SK87296A3 (en) 1997-04-09
KR100399625B1 (en) 2003-12-24
KR960706512A (en) 1996-12-09

Similar Documents

Publication Publication Date Title
CN1070505C (en) Process for the (co) polymerization of olefins
CN1070504C (en) Multistage process for the (co) polymerization of olefins
CN1080268C (en) Catalyst compositions and process for preparing polyolefins
CN1249098C (en) Components and catalysts for polymerizaton of olefins
CN1092669C (en) Components and catalysts for polymerization of olefins
CN1113900C (en) Mixed transition metal catalyst system for olefin polymerization
CN1044372C (en) Solid precursor of a catalytic system for the polymerization of olefins, process for its preparation, catalytic system comprising this solid precursor and process for the polymerization of olefins
US20010023231A1 (en) Components and catalysts for the polymerization of olefins
KR101339550B1 (en) A catalyst for olefin polymerization and co-polymerization and a method for olefin polymerization and co-polymerization with using the same
CN1134710A (en) Components and catalysts for the polymerization of olefins
CN1216088C (en) Process for production of heterophasic polymer compositions and compositions thus obtained
CN1413222A (en) Mixed ziegler/metallocene catalysts for production of bimodal polyolefins
CN1150809A (en) Process for preparation of elastomeric polymer from ethylene, Alpha-olefin and optionally diene
CN1054776A (en) Be used for the catalyzer of olefinic polymerization and prepolymer and by its ethene that makes (being total to) polymkeric substance
CN1267439C (en) Catalyst composition and method of polymerization
CN1296395C (en) Catalyst composition and method for making olefin polymerization and olefin and alpha-loefin copolymerization by using mew-type loaded catalyst system
KR20130057814A (en) A catalyst for olefin polymerization and co-polymerization and a method for olefin polymerization and co-polymerization with using the same

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
C17 Cessation of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20010905

Termination date: 20091102